High-content carbon monoxide conversion system
By designing a series-parallel conversion reactor and catalyst layer structure, combined with steam control, the problem of short catalyst life in high-concentration carbon monoxide conversion was solved, and effective hot spot temperature management and catalyst protection were achieved.
Patent Information
- Application Number
- CN202520363755.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-03-03
- Publication Date
- 2026-02-27
- Estimated Expiration
- 2035-03-03
AI Technical Summary
In existing technologies, high-concentration carbon monoxide conversion reactions result in high hot spot temperatures in the catalyst bed, reducing catalyst lifespan and failing to meet production requirements.
The reactor employs a series-parallel connection of a primary and a secondary conversion reactor. By controlling the catalyst with different CuO contents and water vapor, the gas flow rate is rationally adjusted to control the reaction progress and heat release, thus avoiding catalyst hot spots.
It extends the catalyst's lifespan, effectively controls the reaction hotspot temperature, avoids catalyst sintering, and meets the production requirements of high-concentration carbon monoxide conversion reactions.
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Figure CN223945621U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model belongs to carbon monoxide conversion technical field, concretely relates to a kind of high content carbon monoxide conversion system. BACKGROUND
[0002] CO conversion unit is the important component part of subsequent purification stage in the process of pulverized coal gasification, for processing the raw coal gas generated by pulverized coal gasification device.Currently, most equipment adopts advanced, mature medium conversion string low conversion sulfur conversion process, its process is through conversion catalyst to convert the CO and water vapor generated in the gasification process into H2, CO2.
[0003] CO conversion is important section after the gasification of coal chemical industry, and its process scheme is mature, and currently most of them adopt isothermal conversion and adiabatic conversion two kinds of technology.
[0004] Coal gas, calcium carbide furnace tail gas, iron alloy tail gas, methanol purge gas and other gases contain a large amount of CO and impurities.Taking the large amount of tail gas produced in the process of iron alloy reduction electric furnace production as an example, the effective fuel components such as CO, H2, CH4 in tail gas account for about 80% of the volume of gas, mainly CO, and the calorific value is 2100-2400 kilocalories per standard meter.High concentration of carbon monoxide, especially when the carbon monoxide is converted, the heat release is large, so as to cause the hot spot temperature of catalyst bed to be high, and then reduce the service life of catalyst, which cannot meet the normal production requirements. UTILITY MODEL CONTENT
[0005] The utility model aims at providing a kind of high content carbon monoxide conversion system to solve the above problems existing in prior art.
[0006] In order to achieve the above purpose, the utility model adopts the following technical solutions:
[0007] A high content carbon monoxide conversion system, comprising a raw gas separator, the outlet of the raw gas separator is connected to the inlet of a raw gas filter, the raw gas outlet of the raw gas filter is divided into two gas pipes after passing through a first gas-gas heat exchanger and a raw gas electric heater in turn, one gas pipe is connected to the inlet of a first shift reaction furnace, the other gas pipe is connected to the inlet of a second shift reaction furnace through a first volume flow control valve; the first shift gas outlet of the first shift reaction furnace is divided into two gas pipes after passing through a first gas-gas heat exchanger, one gas pipe is connected to the inlet of a first gas-liquid condenser through a second volume flow control valve, the other gas pipe is connected to the inlet of a second shift reaction furnace after passing through a second gas-gas heat exchanger; the second shift gas outlet of the second shift reaction furnace is connected to the inlet of a first gas-liquid condenser after passing through a second gas-gas heat exchanger, and the outlet of the first gas-liquid condenser is connected to the inlet of a second gas-liquid condenser; the first shift reaction furnace and the second shift reaction furnace are both axial reaction beds filled with low-activity catalyst layers, high-activity catalyst layers and medium-activity catalyst layers from top to bottom in turn, and the outer walls of the first shift reaction furnace and the second shift reaction furnace are both provided with water vapor inlets corresponding to the upper ends of different activity catalyst layers.
[0008] As a preferred technical scheme in the utility model, the water vapor inlets of the first shift reaction furnace are provided with three third volume flow control valves, fourth volume flow control valves and fifth volume flow control valves in front of the three water vapor inlets, and the third volume flow control valves, the fourth volume flow control valves and the fifth volume flow control valves are all connected to a water vapor main pipe.
[0009] As a preferred technical scheme in the utility model, the water vapor inlets of the second shift reaction furnace are provided with three sixth volume flow control valves, seventh volume flow control valves and eighth volume flow control valves in front of the three water vapor inlets, and the sixth volume flow control valves, the seventh volume flow control valves and the eighth volume flow control valves are all connected to the water vapor main pipe.
[0010] As a preferred technical scheme in the utility model, the third volume flow control valves, the fourth volume flow control valves and the fifth volume flow control valves are all connected to the water vapor main pipe through a first water vapor branch pipe, the sixth volume flow control valves, the seventh volume flow control valves and the eighth volume flow control valves are all connected to the water vapor main pipe through a second water vapor branch pipe, a steam electric heater is installed on the water vapor main pipe, and a ninth volume flow control valve is installed on the second water vapor branch pipe.
[0011] As a preferred technical scheme in the utility model, the bottom of the raw gas separator, the raw gas filter, the first gas-liquid condenser and the second gas-liquid condenser is provided with a condensate outlet.
[0012] As one preferred technical scheme in the utility model, the first volume flow control valve, the second volume flow control valve, the third volume flow control valve, the fourth volume flow control valve, the fifth volume flow control valve, the sixth volume flow control valve, the seventh volume flow control valve, the eighth volume flow control valve and the ninth volume flow control valve are all regulating valves.
[0013] Beneficial effects: the utility model adopts the form of series-parallel connection of the first-stage shift reaction furnace and the second-stage shift reaction furnace, controls the gas flow entering each shift reaction furnace through the first volume flow control valve and the second volume flow control valve, reasonably allocates, and prolongs the service life of the catalyst.
[0014] The utility model discloses a first-stage shift reaction furnace and a second-stage shift reaction furnace are filled with shift catalysts with different CuO contents, and the reaction is expanded from a point to a plane, thereby avoiding the concentration of the catalyst at a point to cause heat concentration.
[0015] The utility model discloses a first-stage shift reaction furnace and a second-stage shift reaction furnace are filled with shift catalysts with different CuO contents, and the reaction is expanded from a point to a plane, thereby avoiding the concentration of the catalyst at a point to cause heat concentration. BRIEF DESCRIPTION OF DRAWINGS
[0016] Figure 1 It is the structural schematic diagram of the utility model.
[0017] In the drawing: 1 - raw material gas separator;2 - raw material gas filter;3 - first-stage shift reaction furnace;4 - second-stage shift reaction furnace;5 - first gas-liquid condenser;6 - second gas-liquid condenser;7 - first gas-gas heat exchanger;8 - second gas-gas heat exchanger;9 - raw material gas electric heater;10 - steam electric heater;11 - ninth volume flow control valve;12 - second volume flow control valve;13 - first volume flow control valve;14 - third volume flow control valve;15 - fourth volume flow control valve;16 - fifth volume flow control valve;17 - sixth volume flow control valve;18 - seventh volume flow control valve;19 - eighth volume flow control valve. DETAILED DESCRIPTION
[0018] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the present utility model will be briefly introduced below in conjunction with the accompanying drawings and descriptions of the embodiments or the prior art. Obviously, the following description of the structure of the accompanying drawings is only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. It should be noted that the description of these embodiments is used to help understand this utility model, but does not constitute a limitation on this utility model.
[0019] Example:
[0020] like Figure 1 As shown, this embodiment provides a high-content carbon monoxide conversion system, including a feed gas separator 1. The feed gas of the feed gas separator 1 comes from one or more mixed gases containing high concentrations of carbon monoxide, such as coal gas, calcium carbide furnace tail gas, ferroalloy tail gas, or methanol off-gas. The outlet of the feed gas separator 1 is connected to the inlet of the feed gas filter 2. The feed gas from the outlet of the feed gas filter 2 passes through a first gas-to-gas heat exchanger 7 and a feed gas electric heater 9 in sequence, and is then divided into two gas pipes. One gas pipe connects to the inlet of the first-stage conversion reactor 3, and the other gas pipe connects to the inlet of the second-stage conversion reactor 4 through a first volumetric flow control valve 13. Here, the first-stage conversion reactor 3 and the second-stage conversion reactor 4 are connected in parallel. Then, the gas flow rate entering the first-stage conversion reactor 3 and the second-stage conversion reactor 4 is controlled by the first volumetric flow control valve 13 to reasonably adjust the flow rate and extend the service life of the catalyst. The primary shift gas from the outlet of the primary shift reactor 3 is split into two gas pipes after passing through the first gas-to-gas heat exchanger 7. One gas pipe is connected to the inlet of the first gas-liquid condenser 5 via the second volumetric flow control valve 12, and the other gas pipe is connected to the inlet of the secondary shift reactor 4 via the second gas-to-gas heat exchanger 8. This allows the shift gas from the outlet of the primary shift reactor 3 to be cooled by the first gas-to-gas heat exchanger 7, and then regulated and distributed by the second volumetric flow control valve 12 to control the gas flow into the secondary shift reactor 4. This also realizes the series connection of the primary shift reactor 3 and the secondary shift reactor 4, forming a series-parallel connection. Then, the gas flow rate entering each shift reactor is controlled by the first volumetric flow control valve 13 and the second volumetric flow control valve 12, which allows for more reasonable distribution and extends the service life of the catalyst.
[0021] Based on the above, the secondary shift gas from the outlet of the secondary shift reactor 4 passes through the second gas-to-gas heat exchanger 8 and then connects to the inlet of the first gas-liquid condenser 5. The outlet of the first gas-liquid condenser 5 is connected to the inlet of the second gas-liquid condenser 6 to form the final shift product gas.
[0022] Meanwhile, the first-stage shift reaction furnace 3 and the second-stage shift reaction furnace 4 are both axial reaction beds in which low-activity catalyst layers, high-activity catalyst layers and medium-activity catalyst layers are sequentially filled from top to bottom, and the mass content of CuO in the low-activity catalyst layers is 15-20%, the mass content of CuO in the high-activity catalyst layers is 40-45%, and the mass content of CuO in the medium-activity catalyst layers is 28-32%. By filling the shift catalysts with different CuO contents, the reaction is expanded from a point to a surface, thereby avoiding the concentration of the catalyst at a certain point to cause heat concentration, and the upper ends of the outer walls of the first-stage shift reaction furnace 3 and the second-stage shift reaction furnace 4 corresponding to the different activity catalyst layers are each provided with a water vapor inlet to facilitate the control of the addition of water vapor in the first-stage shift reaction furnace 3 and the second-stage shift reaction furnace 4, control the reaction progress, thereby effectively controlling the heat release of the reaction, and further effectively controlling the hot spot temperature of the catalyst bed, avoiding the sintering of the catalyst at high temperature.
[0023] As a preferred embodiment in the present embodiment, it needs to be further explained that the water vapor inlet of the first-stage shift reaction furnace 3 is provided with three, and the third volume flow control valve 14, the fourth volume flow control valve 15 and the fifth volume flow control valve 16 are respectively arranged in front of the three water vapor inlets, and the third volume flow control valve 14, the fourth volume flow control valve 15 and the fifth volume flow control valve 16 are all connected to the water vapor main pipe to facilitate the accurate control of the addition of water vapor in the first-stage shift reaction furnace.
[0024] As a preferred embodiment in the present embodiment, it needs to be further explained that the water vapor inlet of the second-stage shift reaction furnace 4 is provided with three, and the sixth volume flow control valve 17, the seventh volume flow control valve 18 and the eighth volume flow control valve 19 are respectively arranged in front of the three water vapor inlets, and the sixth volume flow control valve 17, the seventh volume flow control valve 18 and the eighth volume flow control valve 19 are all connected to the water vapor main pipe to facilitate the accurate control of the addition of water vapor in the second-stage shift reaction furnace.
[0025] As a preferred embodiment in the present embodiment, it needs to be further explained that the third volume flow control valve 14, the fourth volume flow control valve 15 and the fifth volume flow control valve 16 are all connected to the water vapor main pipe through the first water vapor branch pipe, and the sixth volume flow control valve 17, the seventh volume flow control valve 18 and the eighth volume flow control valve 19 are all connected to the water vapor main pipe through the second water vapor branch pipe, and the water vapor main pipe is installed with a steam electric heater 10, and the second water vapor branch pipe is installed with a ninth volume flow control valve 11, which can better control the amount of water vapor entering the first-stage shift reaction furnace and the second-stage shift reaction furnace, thereby controlling the reaction progress, and further effectively controlling the heat release of the reaction.
[0026] As a preferred embodiment in the present embodiment, it needs to be further explained that the bottom of the raw gas separator 1, the raw gas filter 2, the first gas-liquid condenser 5 and the second gas-liquid condenser 6 are all provided with a condensate outlet to facilitate the discharge of the process condensate finally formed.
[0027] As a preferred embodiment in the present embodiment, it needs to be further explained that the first volumetric flow control valve 13, the second volumetric flow control valve 12, the third volumetric flow control valve 14, the fourth volumetric flow control valve 15, the fifth volumetric flow control valve 16, the sixth volumetric flow control valve 17, the seventh volumetric flow control valve 18, the eighth volumetric flow control valve 19 and the ninth volumetric flow control valve 11 are all regulating valves, which are mature in technology and convenient to control.
[0028] Experimental Example 1:
[0029] In production, the raw gas is derived from calcium carbide furnace tail gas, and the volume composition is: H2 4.4%, CO 77.8%, CO2 6.2%, N2 11.9%, CH4 0.025%, sulfide 0.02 ppm, chloride 0.003 ppm, arsenide 0 ppm, O2 0.001 ppm.
[0030] The composition of the primary shift gas is H2 69.41%, CO 1.7%, CO2 17.6%, N2 11.24%, CH4 0.027%.
[0031] The composition of the secondary shift gas is H2 69.52%, CO 1.6%, CO2 17.7%, N2 11.25%, CH4 0.028%.
[0032] The total carbon monoxide conversion rate of the primary shift reaction and the secondary shift reaction is 96.1%.
[0033] The shift product gas obtained after cooling, gas-liquid separation and temperature swing adsorption of carbon dioxide of the secondary shift gas has a composition of H2 89.317%, CO 1.24%, CO2 0.15%, N2 9.27%, CH4 0.023%.
[0034] Experimental Example 2:
[0035] In production, the raw gas is derived from iron alloy electric furnace tail gas and coal gas mixed gas, and the volume composition is: H2 11.5%, CO 64.1%, CO2 5.3%, N2 13.6%, CH4 1.4%, sulfide 0.015 ppm, chloride 0.002 ppm, arsenide 0 ppm, O2 0.005 ppm.
[0036] The composition of the primary shifted gas is H2 71.17%, CO 3.2%, CO2 11.5%, N2 12.4%, CH4 1.7%.
[0037] The composition of the secondary shifted gas is H2 72.25%, CO 2.2%, CO2 12.4%, N2 11.9%, CH4 1.25%.
[0038] The total carbon monoxide conversion rate of the primary shift reaction and the secondary shift reaction is 95.58%.
[0039] The shifted product gas is obtained by cooling, gas-liquid separation and temperature swing adsorption of the carbon dioxide from the secondary shifted gas, and the composition of the shifted product gas is H2 88.513%, CO 1.93%, CO2 0.20%, N2 8.26%, CH4 1.10%.
[0040] The utility model discloses a high concentration carbon monoxide shift system, and the process scheme is designed from the reaction mechanism angle, two reaction furnaces are connected in series and parallel, the catalysts with different CuO content are filled, the different water vapour amount is assisted, the progress of reaction is controlled, thereby the heat release of reaction is effectively controlled, and then the hot spot temperature of catalyst bed layer is effectively controlled, the sintering of catalyst under high temperature is avoided, and the raw material gas shift reaction requirement of high concentration carbon monoxide is satisfied.
[0041] Finally, it should be noted that: the above only for the preferred embodiments of the utility model have described, and do not limit the protection scope of the utility model. Any modification, equivalent replacement, improvement etc. within the spirit and principles of the utility model should be included in the protection scope of the utility model.
Claims
1. A high carbon monoxide conversion system, characterized by, The raw gas separator (1) is connected with the inlet of the raw gas filter (2), and the outlet of the raw gas filter (2) is connected with the inlet of the first gas-gas heat exchanger (7) and the raw gas electric heater (9) in sequence, and then is divided into two gas pipes, one of which is connected with the inlet of the first shift reaction furnace (3), and the other of which is connected with the inlet of the second shift reaction furnace (4) through the first volume flow control valve (13). The first shift gas from the outlet of the first shift reaction furnace (3) is connected with the inlet of the first gas-gas heat exchanger (7) and then is divided into two gas pipes, one of which is connected with the inlet of the first gas-liquid condenser (5) through the second volume flow control valve (12), and the other of which is connected with the inlet of the second shift reaction furnace (4) through the second gas-gas heat exchanger (8). The second shift gas from the outlet of the second shift reaction furnace (4) is connected with the inlet of the first gas-liquid condenser (5) through the second gas-gas heat exchanger (8), and the outlet of the first gas-liquid condenser (5) is connected with the inlet of the second gas-liquid condenser (6). The first shift reaction furnace (3) and the second shift reaction furnace (4) are both axial reaction beds filled with low-activity catalyst layer, high-activity catalyst layer and medium-activity catalyst layer from top to bottom, and the outer wall of the first shift reaction furnace (3) and the outer wall of the second shift reaction furnace (4) are both provided with water vapor inlets corresponding to the upper end of different activity catalyst layers.
2. A high carbon monoxide shift system according to claim 1, wherein, The water vapor inlets of the first shift reaction furnace (3) are provided with three third volume flow control valves (14), fourth volume flow control valves (15) and fifth volume flow control valves (16) in sequence, and the third volume flow control valves (14), the fourth volume flow control valves (15) and the fifth volume flow control valves (16) are all connected with the water vapor main pipe.
3. A high carbon monoxide shift system according to claim 2, wherein, The water vapor inlets of the second shift reaction furnace (4) are provided with three sixth volume flow control valves (17), seventh volume flow control valves (18) and eighth volume flow control valves (19) in sequence, and the sixth volume flow control valves (17), the seventh volume flow control valves (18) and the eighth volume flow control valves (19) are all connected with the water vapor main pipe.
4. A high carbon monoxide shift system according to claim 3, wherein, The third volume flow control valves (14), the fourth volume flow control valves (15) and the fifth volume flow control valves (16) are all connected with the water vapor main pipe through the first water vapor branch pipe, the sixth volume flow control valves (17), the seventh volume flow control valves (18) and the eighth volume flow control valves (19) are all connected with the water vapor main pipe through the second water vapor branch pipe, the water vapor main pipe is provided with a steam electric heater (10), and the second water vapor branch pipe is provided with a ninth volume flow control valve (11).
5. A high carbon monoxide shift system according to any one of claims 1-4, characterized in that, The bottom of the raw gas separator (1), the raw gas filter (2), the first gas-liquid condenser (5) and the second gas-liquid condenser (6) are all provided with condensate outlets.
6. The high CO content shift system of claim 1, wherein, The first volume flow control valve (13), the second volume flow control valve (12), the third volume flow control valve (14), the fourth volume flow control valve (15), the fifth volume flow control valve (16), the sixth volume flow control valve (17), the seventh volume flow control valve (18), the eighth volume flow control valve (19) and the ninth volume flow control valve (11) are each a regulating valve.